WO2018168023A1 - 好気性生物処理方法 - Google Patents
好気性生物処理方法 Download PDFInfo
- Publication number
- WO2018168023A1 WO2018168023A1 PCT/JP2017/033547 JP2017033547W WO2018168023A1 WO 2018168023 A1 WO2018168023 A1 WO 2018168023A1 JP 2017033547 W JP2017033547 W JP 2017033547W WO 2018168023 A1 WO2018168023 A1 WO 2018168023A1
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- oxygen
- treatment method
- biological treatment
- water
- membrane
- Prior art date
Links
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/20—Activated sludge processes using diffusers
- C02F3/208—Membrane aeration
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/08—Aerobic processes using moving contact bodies
- C02F3/085—Fluidized beds
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
- B01D65/08—Prevention of membrane fouling or of concentration polarisation
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
- B01F21/00—Dissolving
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/08—Aerobic processes using moving contact bodies
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/10—Packings; Fillings; Grids
- C02F3/104—Granular carriers
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/10—Packings; Fillings; Grids
- C02F3/105—Characterized by the chemical composition
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1268—Membrane bioreactor systems
- C02F3/1273—Submerged membrane bioreactors
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/20—Activated sludge processes using diffusers
- C02F3/201—Perforated, resilient plastic diffusers, e.g. membranes, sheets, foils, tubes, hoses
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/26—Activated sludge processes using pure oxygen or oxygen-rich gas
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2311/00—Details relating to membrane separation process operations and control
- B01D2311/26—Further operations combined with membrane separation processes
- B01D2311/2688—Biological processes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2315/00—Details relating to the membrane module operation
- B01D2315/06—Submerged-type; Immersion type
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
- B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
- B01D65/04—Membrane cleaning or sterilisation ; Membrane regeneration with movable bodies, e.g. foam balls
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F2003/001—Biological treatment of water, waste water, or sewage using granular carriers or supports for the microorganisms
- C02F2003/003—Biological treatment of water, waste water, or sewage using granular carriers or supports for the microorganisms using activated carbon or the like
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/32—Nature of the water, waste water, sewage or sludge to be treated from the food or foodstuff industry, e.g. brewery waste waters
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
- C02F2103/34—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32
- C02F2103/346—Nature of the water, waste water, sewage or sludge to be treated from industrial activities not provided for in groups C02F2103/12 - C02F2103/32 from semiconductor processing, e.g. waste water from polishing of wafers
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2303/00—Specific treatment goals
- C02F2303/20—Prevention of biofouling
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/10—Packings; Fillings; Grids
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Definitions
- the present invention relates to a method for aerobic biological treatment of organic treated water, and in particular, a MABR (membrane aeration bioreactor) system in which oxygen is dissolved in treated water in a reaction tank using an oxygen-dissolving membrane.
- the present invention relates to an aerobic biological treatment method.
- the aerobic biological treatment is performed by dissolving oxygen in the water to be treated by an oxygen dissolving membrane.
- an oxygen-dissolving membrane a hollow fiber membrane is often used as in Patent Document 1.
- An object of the present invention is to provide an aerobic biological treatment method capable of keeping the oxygen supply rate of an oxygen-dissolved film high by preventing the organism from adhering to the oxygen-dissolved film.
- the gist of the present invention is as follows.
- an aerobic biological treatment method in which oxygen is dissolved in water to be treated in the reaction tank by an oxygen-dissolving film disposed in the reaction tank, and the water to be treated is aerobic biologically treated.
- An aerobic biological treatment method characterized in that adhesion of a living organism to the oxygen-dissolving membrane is prevented by suspending or flowing an adhesion carrier.
- biofouling on the oxygen-dissolved membrane is prevented (including suppression) by suspension or flow of the biofouling carrier.
- a remarkably high oxygen dissolution rate can be obtained stably.
- the pressure required for oxygen dissolution is the same as before.
- the MLSS concentration in the reaction tank by increasing the MLSS concentration in the reaction tank to 10,000 mg / L or more, it is possible to prevent organisms from attaching to the oxygen-dissolved film.
- the amount of aeration required for mixing the MLSS is 1/20 or less of the amount of aeration for supplying oxygen, and the power cost is negligibly low.
- FIG. 1 It is a typical longitudinal cross-sectional view of the reaction apparatus which shows the aerobic biological treatment method of this invention.
- 2 is an explanatory diagram of Embodiment 1.
- FIG. It is explanatory drawing of Example 2, 3 and the comparative example 1.
- FIG. 1 is a schematic longitudinal sectional view of a reaction apparatus in which the aerobic biological treatment method of the present invention is performed.
- an oxygen-dissolved membrane module 2 is installed in a reaction tank 3.
- One or a plurality of oxygen-dissolving membrane modules 2 are installed.
- the oxygen-dissolving membrane module 2 may be installed in multiple upper and lower stages.
- Raw water is supplied to the bottom of the reaction tank 3 by the pipe 4 and the nozzle 5 to form a fluidized bed F of a carrier such as activated carbon.
- the treated water that has passed through the fluidized bed F overflows the trough 6 and flows out from the outlet 7.
- the oxygen-dissolving membrane module 2 includes a non-porous oxygen-dissolving membrane, and oxygen that has permeated through the membrane is dissolved in the water to be treated in the reaction tank 3, so that no bubbles are generated in the reaction tank 3.
- Air may flow from the top to the bottom of the oxygen-dissolving membrane module 2, may flow from the bottom to the top, or may flow in the lateral direction.
- a plurality of oxygen-dissolving membranes When a plurality of oxygen-dissolving membranes are ventilated, they may be ventilated in series or in parallel.
- the carrier is preferably a bioadhesive carrier such as activated carbon, zeolite, sand, sponge, plastic, cellulose, gel (for example, PVA, PEG, polyurethane, polyethylene, etc.), rubber or the like.
- a bioadhesive carrier such as activated carbon, zeolite, sand, sponge, plastic, cellulose, gel (for example, PVA, PEG, polyurethane, polyethylene, etc.), rubber or the like.
- the true specific gravity of the bioadhesive carrier is preferably about 0.9 to 2.5, particularly preferably 1.0 to 2.0.
- the size of the bioadhesive carrier is preferably about 0.1 mm to 20 mm, particularly preferably about 0.2 mm to 5 mm.
- the bioadhesive carrier is preferably added in an amount of 1 to 50%, particularly 5 to 40% of the reaction tank volume.
- a fluidized bed of the carrier is formed, but the carrier may be suspended.
- the carrier is preferably suspended or fluidized by one or more of aeration of the liquid in the reaction vessel, flow of the liquid, and mechanical operation.
- the MLSS concentration in the reaction tank is maintained at 10,000 mg / L or more, preferably 10,000 to 50,000 mg / L, particularly preferably 20,000 to 30,000 mg / L.
- the MLSS concentration is usually about 600 to 6000 mg / L (for example, about 800 to 2000 mg / L for sewage and about 4000 to 6000 mg / L for industrial wastewater).
- oxygen can be added by adding a carrier.
- the supply speed can be kept high.
- a filtration membrane in the treatment liquid in the reaction tank and take out the permeated water of this filtration membrane as the treatment water.
- the method of the present invention is suitable for treating water such as semiconductor manufacturing wastewater, liquid crystal manufacturing wastewater, chemical process wastewater, food manufacturing wastewater, and sewage.
- the oxygen-dissolving membrane of the oxygen-dissolving membrane module 2 may be any of a hollow fiber membrane, a flat membrane, and a spiral membrane, but a hollow fiber membrane is preferable.
- a hollow fiber membrane is preferable.
- a composite film having a high strength and a porous hollow fiber coated with a nonporous polymer may be used.
- the hollow fiber membrane preferably has an inner diameter of 0.05 to 4 mm, particularly 0.2 to 1 mm, and a thickness of 0.01 to 0.2 mm, particularly 0.02 to 0.1 mm. If the inner diameter is smaller than this, the aeration pressure loss is large, and if it is larger, the surface area becomes smaller and the oxygen dissolution rate decreases. When the thickness is smaller than the above range, the physical strength is reduced and the film is easily broken. On the other hand, when the thickness is larger than the above range, the oxygen permeation resistance increases and the oxygen dissolution efficiency decreases.
- the length of the hollow fiber membrane is preferably about 0.5 to 3 m, particularly preferably about 1 to 2 m. If the hollow fiber membrane is too long, when a large amount of biofilm adheres, problems such as breakage, solidification into a dumpling, a decrease in surface area, a decrease in oxygen dissolution efficiency, and an increase in pressure loss occur. If the hollow fiber membrane is too short, the cost increases. For the same reason, the length of the flat membrane and the spiral membrane is preferably 0.5 to 1.5 m.
- Example 1 (Prevention of biofilm adhesion by carrier fluidized bed) As shown in FIG. 2, 25 mL of crushed charcoal (not shown) having an average diameter of 0.7 mm (JIS mesh) is placed in a transparent PVC pipe 11 having an inner diameter of 13 mm and a length of 500 mm, and an inner diameter of 0.5 mm and an outer diameter as an oxygen-dissolving film. Eight 0.7 mm silicon tubes 12 were inserted, and the top and bottom of the PVC tube 11 were sealed. Air was bubbled through the silicon tube 12 at 15 mL / min. The inlet pressure was 5 kPa.
- the transparent PVC pipe 11 is supplied with synthetic waste water (NH 4 -N 400 mg / L, NaHCO 3 : 800 mg / L, K 2 HPO 4 : 100 mg / L) in the raw water tank 13 by a pump 14 and pipes 15 and 16 at 40 mL / min.
- the water was circulated through the raw water tank 13 and the transparent PVC pipe 11.
- the crushed coal flowed by this water flow.
- a pH meter 17 was installed in the raw water tank 13, and an aqueous NaOH solution was added from the chemical liquid tank 19 by a chemical injection pump 18 so that the pH did not become 7 or less.
- the operation was continued for 2 months under the above conditions.
- the oxygen concentration in the outlet gas of the silicon tube 12 was an average of 10.2%, and the oxygen dissolution efficiency was about 50%.
- the NH 4 —N of the treated water was below the detection limit (50 ⁇ g / L).
- Example 2 (Prevention of biofilm adhesion by increasing MLSS concentration)
- nitrified sludge is added to a 3 L transparent PVC aeration tank 31 so as to be 10,000 mg / L, and a silicon tube having an inner diameter of 0.5 mm, an outer diameter of 0.7 mm, and a length of 30 cm.
- An oxygen-dissolving membrane module 32 in which 800 pieces were bundled was installed.
- the air was passed through the oxygen-dissolving membrane module 32 at 150 mL / min.
- the inlet pressure was 5 kPa.
- Aeration was performed at an air amount of 6 L / min for 10 seconds from the air diffusion tube 33 at the bottom of the aeration tank once every 2 minutes.
- Example 2 The same synthetic waste water as in Example 1 was passed through the aeration tank 31 at 7 mL / min.
- an MF flat membrane solid-liquid separator 34 was installed, and the filtrate was discharged from the pipe 35 as a treatment liquid.
- Example 1 As shown in FIG. 3B, the same apparatus as in Example 2 was operated except that the MF flat membrane solid-liquid separator 34 was removed from the apparatus of FIG. Aeration was performed at a frequency of once every 2 minutes at 1 L / min for 10 seconds. Other conditions were the same as in Example 2.
- Example 3 (Prevention of biofilm adhesion by fluid carrier) As shown in FIG. 3 (c), 1 L of 3 mm square polyurethane sponge was added to the aeration tank using the same reactor as in FIG. 3 (b). In the aeration tank, a screen is provided as a carrier separating means for preventing the sponge (carrier) from flowing out in the vicinity of the water intake portion of the pipe 35. A mixed solution of raw water and treated water was passed through the circulating water tank 40 at a rate of 70 mL / min from the circulating water tank 40 in an upward flow from the raw water supply pipe 42 installed at the bottom of the tank so that the polyurethane sponge flows. Aeration was performed at a frequency of once per minute for 5 seconds at 1 L / min.
- the ammonia concentration in the treatment liquid from the pipe 35 was 0 to 20 mg / L.
- the oxygen supply rate of the silicon film was 45 to 55 g-O 2 / m 2 / day.
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Water Supply & Treatment (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Organic Chemistry (AREA)
- Microbiology (AREA)
- Biodiversity & Conservation Biology (AREA)
- Chemical Kinetics & Catalysis (AREA)
- General Chemical & Material Sciences (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Biological Treatment Of Waste Water (AREA)
- Aeration Devices For Treatment Of Activated Polluted Sludge (AREA)
Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
US16/492,834 US20200148566A1 (en) | 2017-03-16 | 2017-09-15 | Aerobic biological treatment method |
EP17900702.6A EP3597608A4 (en) | 2017-03-16 | 2017-09-15 | AEROBIC TREATMENT PROCESS |
CN201780082066.1A CN110139836A (zh) | 2017-03-16 | 2017-09-15 | 好氧性生物处理方法 |
SG11201908301P SG11201908301PA (en) | 2017-03-16 | 2017-09-15 | Aerobic biological treatment method |
KR1020197011070A KR20190125284A (ko) | 2017-03-16 | 2017-09-15 | 호기성 생물 처리 방법 |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP2017-051092 | 2017-03-16 | ||
JP2017051092A JP6365714B1 (ja) | 2017-03-16 | 2017-03-16 | 好気性生物処理方法 |
Publications (1)
Publication Number | Publication Date |
---|---|
WO2018168023A1 true WO2018168023A1 (ja) | 2018-09-20 |
Family
ID=63036746
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/JP2017/033547 WO2018168023A1 (ja) | 2017-03-16 | 2017-09-15 | 好気性生物処理方法 |
Country Status (8)
Country | Link |
---|---|
US (1) | US20200148566A1 (zh) |
EP (1) | EP3597608A4 (zh) |
JP (1) | JP6365714B1 (zh) |
KR (1) | KR20190125284A (zh) |
CN (1) | CN110139836A (zh) |
SG (1) | SG11201908301PA (zh) |
TW (1) | TWI764935B (zh) |
WO (1) | WO2018168023A1 (zh) |
Families Citing this family (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JP7437139B2 (ja) * | 2019-11-19 | 2024-02-22 | 住友重機械エンバイロメント株式会社 | 水処理装置及び水処理方法 |
Citations (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS497992B1 (zh) | 1968-10-22 | 1974-02-23 | ||
JPS6490093A (en) * | 1987-10-01 | 1989-04-05 | Komatsu Mfg Co Ltd | Apparatus for treating waste water |
JPH0568990A (ja) * | 1991-09-17 | 1993-03-23 | Japan Organo Co Ltd | 透過膜中空散気体を内蔵する濾過装置 |
JP2003211185A (ja) * | 2002-01-25 | 2003-07-29 | Hiroshima Pref Gov | 無動力排水処理方法 |
US6616843B1 (en) * | 1998-12-18 | 2003-09-09 | Omnium De Traitement Et De Valorisation | Submerged membrane bioreactor for treatment of nitrogen containing water |
JP2005034739A (ja) * | 2003-07-15 | 2005-02-10 | Mitsubishi Rayon Co Ltd | 排水処理方法 |
JP2006101805A (ja) * | 2004-10-07 | 2006-04-20 | Japan Organo Co Ltd | 中空糸膜型バイオリアクターおよびそれを用いた液体処理方法 |
JP2008221070A (ja) * | 2007-03-09 | 2008-09-25 | Kurita Water Ind Ltd | 気液接触装置及び気液接触方法 |
WO2015132291A1 (en) * | 2014-03-04 | 2015-09-11 | Oxymem Limited | A membrane aerated biofilm reactor (mabr) |
JP2017051092A (ja) | 2015-09-04 | 2017-03-09 | 周 文三 | モータの放熱構造 |
Family Cites Families (13)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS5143252B2 (zh) | 1972-05-13 | 1976-11-20 | ||
DE3544383A1 (de) * | 1985-07-17 | 1987-01-29 | Ivan Sekoulov | Verfahren zur biologischen und/oder physikalischen elimination unerwuenschter wasserinhaltsstoffe aus wasser mittels gefluteter biofilmreaktoren u. anlage zur durchfuehrung des verfahrens |
DE3544382A1 (de) * | 1985-12-14 | 1987-06-19 | Ivan Prof Dr Ing Sekoulov | Verfahren zur sauerstoffversorgung von bioreaktoren und vorrichtung zur durchfuehrung des verfahrens und die anwendung der vorrichtung |
JPS63156514A (ja) * | 1986-12-18 | 1988-06-29 | Daikin Ind Ltd | 発酵槽用の酸素富化機 |
US5352610A (en) * | 1990-03-22 | 1994-10-04 | Braeutigam Hans Juergen | Tubular membrane assembly |
US5262320A (en) * | 1990-06-18 | 1993-11-16 | Massachusetts Institute Of Technology | Cell-culturing apparatus and method employing a macroporous support |
JPH0568996A (ja) * | 1991-05-17 | 1993-03-23 | Nippon Plant:Kk | 溶存気体の発生方法及びその溶存気体を用いた汚水処理装置 |
DE19528871C2 (de) * | 1994-08-24 | 1997-08-14 | Forschungszentrum Juelich Gmbh | Begasungs-Rohrmodul mit selektiv gasdurchlässiger Schlauchmembranen und damit versehene Reaktoren für Zellkulturtechnik sowie Wirbelschicht-Reaktoren für Zellkultivierung |
US7300571B2 (en) * | 2003-02-13 | 2007-11-27 | Zenon Technology Partnership | Supported biofilm apparatus |
CN101198555A (zh) * | 2005-06-15 | 2008-06-11 | 财团法人电力中央研究所 | 微生物活性控制物质供给方法及其装置以及利用该装置的环境净化方法及生物反应器 |
JP5358886B2 (ja) * | 2007-02-22 | 2013-12-04 | 栗田工業株式会社 | 有機物含有水の生物処理方法 |
JP5883698B2 (ja) * | 2012-03-29 | 2016-03-15 | 水ing株式会社 | 排水処理方法 |
CN205914031U (zh) * | 2016-06-27 | 2017-02-01 | 河北工程大学 | 一种防止中空纤维膜生物反应器膜堵塞的实验系统 |
-
2017
- 2017-03-16 JP JP2017051092A patent/JP6365714B1/ja active Active
- 2017-09-15 CN CN201780082066.1A patent/CN110139836A/zh active Pending
- 2017-09-15 US US16/492,834 patent/US20200148566A1/en not_active Abandoned
- 2017-09-15 SG SG11201908301P patent/SG11201908301PA/en unknown
- 2017-09-15 WO PCT/JP2017/033547 patent/WO2018168023A1/ja unknown
- 2017-09-15 KR KR1020197011070A patent/KR20190125284A/ko not_active Application Discontinuation
- 2017-09-15 EP EP17900702.6A patent/EP3597608A4/en not_active Withdrawn
- 2017-09-26 TW TW106132878A patent/TWI764935B/zh active
Patent Citations (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS497992B1 (zh) | 1968-10-22 | 1974-02-23 | ||
JPS6490093A (en) * | 1987-10-01 | 1989-04-05 | Komatsu Mfg Co Ltd | Apparatus for treating waste water |
JPH0568990A (ja) * | 1991-09-17 | 1993-03-23 | Japan Organo Co Ltd | 透過膜中空散気体を内蔵する濾過装置 |
US6616843B1 (en) * | 1998-12-18 | 2003-09-09 | Omnium De Traitement Et De Valorisation | Submerged membrane bioreactor for treatment of nitrogen containing water |
JP2003211185A (ja) * | 2002-01-25 | 2003-07-29 | Hiroshima Pref Gov | 無動力排水処理方法 |
JP2005034739A (ja) * | 2003-07-15 | 2005-02-10 | Mitsubishi Rayon Co Ltd | 排水処理方法 |
JP2006101805A (ja) * | 2004-10-07 | 2006-04-20 | Japan Organo Co Ltd | 中空糸膜型バイオリアクターおよびそれを用いた液体処理方法 |
JP2008221070A (ja) * | 2007-03-09 | 2008-09-25 | Kurita Water Ind Ltd | 気液接触装置及び気液接触方法 |
WO2015132291A1 (en) * | 2014-03-04 | 2015-09-11 | Oxymem Limited | A membrane aerated biofilm reactor (mabr) |
JP2017051092A (ja) | 2015-09-04 | 2017-03-09 | 周 文三 | モータの放熱構造 |
Non-Patent Citations (1)
Title |
---|
See also references of EP3597608A4 |
Also Published As
Publication number | Publication date |
---|---|
TW201834975A (zh) | 2018-10-01 |
CN110139836A (zh) | 2019-08-16 |
TWI764935B (zh) | 2022-05-21 |
KR20190125284A (ko) | 2019-11-06 |
JP2018153733A (ja) | 2018-10-04 |
EP3597608A4 (en) | 2020-12-02 |
US20200148566A1 (en) | 2020-05-14 |
EP3597608A1 (en) | 2020-01-22 |
SG11201908301PA (en) | 2019-10-30 |
JP6365714B1 (ja) | 2018-08-01 |
Similar Documents
Publication | Publication Date | Title |
---|---|---|
US20070235385A1 (en) | Aerated Anoxic Membrane Bioreactor | |
JP2008221070A (ja) | 気液接触装置及び気液接触方法 | |
WO2019159667A1 (ja) | 好気性生物処理装置 | |
JP2003024985A (ja) | 脱窒装置及び脱窒方法 | |
JP2003053363A (ja) | 有機物含有水の処理方法及び処理装置 | |
WO2018168023A1 (ja) | 好気性生物処理方法 | |
KR20190022388A (ko) | 유동상 생물반응조에서 담체 순환 및 유실 방지를 위한 장치 | |
WO2019163429A1 (ja) | 好気性生物処理装置の運転方法 | |
TW201940687A (zh) | 好氧生物處理裝置 | |
JP6899104B2 (ja) | 排水処理方法および排水処理装置 | |
WO2019163428A1 (ja) | 好気性生物処理装置及びその運転方法 | |
WO2019163422A1 (ja) | 好気性生物処理装置の運転方法 | |
KR20030097075A (ko) | 생물막활성탄과 마이크로필터모듈을 이용한 오·폐수고도처리장치 | |
JP6614253B2 (ja) | 好気性生物処理装置及びその運転方法 | |
WO2015002121A1 (ja) | 汚水浄化処理方法及び汚水浄化処理装置 | |
JP6610688B2 (ja) | 好気性生物処理装置 | |
JP4181501B2 (ja) | 生物膜濾過装置及び方法 | |
WO2019163427A1 (ja) | 好気性生物処理装置 | |
JP2024085958A (ja) | 液体処理装置及び処理方法 | |
JP2006289370A (ja) | 固液分離方法及び装置 | |
JP2004330076A (ja) | 活性汚泥混合液の固液分離方法及び装置 |
Legal Events
Date | Code | Title | Description |
---|---|---|---|
121 | Ep: the epo has been informed by wipo that ep was designated in this application |
Ref document number: 17900702 Country of ref document: EP Kind code of ref document: A1 |
|
ENP | Entry into the national phase |
Ref document number: 20197011070 Country of ref document: KR Kind code of ref document: A |
|
NENP | Non-entry into the national phase |
Ref country code: DE |
|
ENP | Entry into the national phase |
Ref document number: 2017900702 Country of ref document: EP Effective date: 20191016 |